Emulsion treaters and emulsion treating methods



Nov. 21, 1961 c. o. GLASGOW 3,

EMULSION TREATERS AND EMULSION TREATING METHODS Filed Feb. 16, 1959 4Sheets-Sheet 1 FUEL GAS

INLET INLET WATER 0U T L ET -COOLANT COOL/1 N T GAS OUTLET INVENTOR. CLAQENCE O. GLASGO W wad/KM ATTORNEY Nov. 21, 1961 c. o. GLASGOW 3,009,536

EMULSION TREATERS AND EMULSION TREATING METHODS 4 Sheets-Sheet 2 FiledFeb. 16, 1959 INVENTOR. CLARENCE O. GLASGOW z lj/xz ATTORNEY Nov. 21,1961 c. o. GLASGOW EMULSION TREATERS AND EMULSION TREATING METHODS FiledFeb. 16, 1959 4 Sheets-Sheet 5 n I I l I l l n INVENTOR.

CL AREA/CE 0. GLASGOW ATTORNEY Nov. 21, 1961 c. o. GLASGOW 3,009,536

EMULSION TREATERS AND EMULSION TREATING METHODS Filed Feb. 16, 1959 4Sheets-Sheet 4 FUEL 6A8 INLET INVENTOR. CLARENCE 0. GLASGOW A T TORNE YUnited States Patent 3,009,536 EMULSION TREATERS AND EMULSION TREATINGMETHODS Clarence 0. Glasgow, Tulsa, Okla., assignor to National TankCompany, Tulsa, Okla, a corporation of Nevada Filed Feb. 16, 1959, Ser.No. 793,596 39 Claims. (Cl. 183--2.7)

The present invention relates to emulsion treaters and emulsion treatingmethods. The invention is particularly concerned with processing oilwell production in the field in order to separate the production intooil, water and Oil well production varies widely in quality, betweenlocalities. Some black asphaltic base crude oil production in variousparts of the world has relatively little gaseous phase and its gravityis low, in the order of 25 or 30 API to 9 or 10 A91. This productionoften has a great deal of foam. Also the tuiion between the water andoil is relatively strong, or tight. On start-up, during intermittenttreating operation, the low gravity production is diflicult to melt fromits congealed condition in the treating apparatus, particularly thecoalescing section. The foam is difficult to reduce quickly andeffectively. When a single source of heat is applied to the productionto break the tight emulsion, the skin temperature of the heat sourcemust be developed so high that thermal decomposition of the hydrocarbonsresults in coking of the surface of the heat source. Also, if theproduction is not passed over the heat source with relatively longresidence time, and there is a relatively high skin temperaturerequired, thermal agitation will not be developed with which to wet thesurace of the heat source and prevent vaporization of themineralcarrying water of the production, leaving scale deposits on thesurface of the heat source.

Another problem met in areas producing these black asphaltic base crudeemulsions is a dimentional one of the apparatus in which the process iscarried out. Local ordinances may prohibit these structures extending ashigh as .a common vertical treating vessel. The lease owner may wish tocooperate with civic programs to shield unsightly treating apparatusfrom the public gaze. Also, in remote areas, labor may not be avail-ablewith which to set the vertical structures. Therefore, the peculiartreating problems of these productions have added the problem solvingthe treating problems in apparatus which is horizontally arranged.

A primary object of the present invention is to apply a source of heatso as to reduce the foam of oil well production effectively at thebeginning of its treating process.

Another object is to supply heat to oil well production so as to greatlyreduce, or eliminate, coking and/ or scaling on the surface of a heatsource.

Another object is to mechanically manipulate oil well production andapply heat to it at a plurality of locations so as to thoroughly mix theproduction with any emulsion-breaking chemical that may have been addedand raise the temperature of the production to where it is completelyprepared for optimum coalescence of its water and oil.

Another object is to conserve the gravity of the final clean oil productby condensing all liquefiable components of the gas evolved from theproduction prior to coalescence of the water and oil while preventingcondensation of water vapor from gas above the clean oil back into theclean oil as it is removed from the procms.

Another object is to develop a differential between the pressures onsurfaces of liquids in the treating process to move the productionliquids through the steps of the process.

Another object is to provide a structural arrangement for vesselcompartments in which the treating process takes place, the vesselcompartments being in substantial horizontal alignment.

The present invention contemplates treating a lowgravity, highviscosity, foamy oil well production by initially heating the productionby dispersing it in a body of water which has been heated enough toeffectively reduce the foam and militate against its thermaldecomposition in coking on the surface of a subsequent heat source.

The invention further contemplates the initial heating being controlledto reduce the viscosity of the production sufficiently to raise theefficiency of heat transfer from the heat source to the productionenough that the skin temperature of a subsequent heating source need notbe so high that it will cause thermal decomposition of hydrocarbons onits surface.

The invention further contemplates that bafiies mounted in the body ofwater will mechanically manipulate the production in spreading theproduction washed therein into thin sheets from which the lighterhydrocarbon gas will readily evolve, or breakout, in foam reduction andgas release and which will cause the production to heat more eflicientlyin viscosity reduction and which will cause the production to mix morethoroughly with any emulsion-breaking chemical added.

The invention further contemplates the initial heating being followed bya second heating with a source of heat hot enough, in a body of theproduction large enough, to set up thermal currents which thoroughlyagitate the body of production in completing the mixing with thechemical and raising it to the temperature where it is completelyprepared for optimum coalescence of its water and oil. The production isflowed downwardly over the second source of heat so the final stage ofdegassing is accomplished in the upper region of the body of productionand disturbance from degassing is kept to a minimum. The production hasbeen reduced in viscosity by the first heating so the skin temperatureof the second heat source need not be high enough to result in scalingand coking in getting the production up to the final treatingtemperature.

The invention further contemplates the gas evolved from the plural stageheating being conducted through a heat exchanger in which a cool streamof fluid condenses all liquefiable components of the gas and the liquidsare returned to the production passing downwardly over the second heatsource to maintain the gravity of the final clean oil product. Theremaining unliquefied gas is passed over the surface of theclean oilproduct, combining with any gas evolved above its surface. However, theliquids passed from the initial heating to the subsequent heating areheat-exchanged with the gas'to prevent condensation of any water vaportherefrom into the clean oil.

The invention further contemplates sensing the level of liquids floweddownwardly over the second source of heat and controlling thewithdrawing of the gas evolved from the liquids of the production heatedin developing a difierential between the pressure on the surface ofliquids heated and the pressure on the clean oil to move clean oil fromthe process to storage or use, and at any desirable working pressurewithin the safe range of the vessel.

The present invention further contemplates a series of separate vesselcompartments, one compartment providing the body of heated water,another compartment providing the collection of the well stream largeenough to give the required residence time and thermal agitation. Andanother compartment providing the treating coalescence. The compartmentsare normally within a single vessel and in horizontal alignment.However, the compartments can be in separate vessels, connected byconduits.

The invention further contemplates placing the treating coalescencecompartment between the other two compartments in a horizontal vessel sothe connecting passage between the other two compartments willheat-exchange with the top of the treating coalescence compartment tokeep the gas above the clean oil warm enough to prevent water vapor inthe gas from condensing into the clean oil.

Other objects, advantages and features of this invention will becomemore apparent to one skilled in the art upon consideration of thewritten specification, appended claims, and the attached drawingswherein;

FIG. 1 is a diagrammatic sectioned elevation of a vessel embodying theinvention.

FIG. 2 is a section along lines 2-2 of FIG. 1.

FIG. 3 is a diagrammatic sectioned elevation of a modification of theFIG. 1 vessel embodying the invention.

FIG. 4 is a section along lines 4-4 of FIG. 3.

Referring specifically to FIG. 1, there is shown the essentialcomponents of an oil well production treater. With the components ofthis treater as disclosed, the process of the invention may be carriedout. A quite diagrammatic style of illustration has been utilized forboth simplicity and clarity.

The treater of FIG. 1 is characterized by a shell 1 to which theproduction of an oil Well is brought in conduit 2. Conduit 2 introducesthe production into first compartment 3 within shell 1.

Compartment 3 is essentially defined in one end of shell 1 by partition4. A conventional form of gas-fired heater 5 is mounted withincompartment 3. The combustion of gas within the tube of heater 5 isautomatically controlled by a system responding to the temperaturesensed by element 6. Element 6 is inserted directly into compartment 3,being immersed in the liquid within compartment 3 which is heated by thetube of heater 5.

It is contemplated that a body of water will fill compartment 3. The oilwell production introduced into compartment 3 by conduit 2 will bedispersed through the body of heated Water by conventional spreaderstructure illustrated at 7. Free water will drop out of the productionrapidly in compartment 3, maintaining the inventory of water therein.Surplus water constantly overflows from compartment 3, along with oilWell production heated thereby.

The body of water, heated as it is, to within a predeterminedtemperature range, starts the treating process. Lowgravity,high-viscosity, foamy oil Well production, dispersed through the body ofheated water, is brought up to temperature by contact with the wateruntil the viscosity of the production is lowered a desired amount.

When the viscosity of the production is lowered the desired amount, thefoam of the production will be reduced because of the weakening of thevapor tension of the gas bubbles which make up the foam. Additionally,the viscosity reduction will raise the heat transfer rate between theproduction and the heating structures of the process. These results arebrought about by close regulation of heater 5 with the control system ofelement 6 in bringing the temperature of the production, dispersed upthrough the water of compartment 3, within the predetermined temperaturerange.

Baffies 8 represent additional structure within compartment 3 whichcontributes to the new results attained by the invention. The baifies 8represent structure used to prolong the travel time of the dispersedemulsion up through the body of heated Water. These bafiles will spreadthe emulsion into relatively thin sheets as the production is heated.Spreading the production in this manner reduces the break-out time ofgas bubbles within the production. Further, this function of spreadingthe production into thin sheets promotes the efficiency of heattransfer, by conduction, from the water to the dispersed emulsion. Ofcourse, as the travel of emulsion through the water washing bath isprolonged by its serpentine path upward through compartment 3, there isgreater opportunity for the heat of the water bath to raise thetemperature of the producion. Additionally, the bafile structure, inspreading and re-spreading the emulsion into thin sheets, agitates theproduction and any chemical which may have been added thereto. Theresult is the beginning of a thorough mixing process which brings theemulsion and emulsion-breaking chemical into close contact so thechemical may function efficiently.

After passing up through compartment 3, the production passes out of thecompartment through opening 9. Opening 9 is defined between theright-end head of shell 1 and an end of elongated partition 10 runningalmost the length of shell 1. With the upper walls of shell 1,horizontal partition 10 forms an elongated passage along the top ofshell 1. Through this elongated passage passes heated water ofcompartment 3, the production, and any emulsion-breaking chemical thatmay have been added thereto. The gaseous components of the productionwhich have been evolved in compartment 3 are also passed out of opening9. All of these products from compartment 3 are passed down theelongated passage, over partition 10, to a second compartment in theopposite end of shell 1. During their passage along partition 10, theheated water, emulsion and chemical are given an opportunity to mix morethoroughly, bringing the temperature of the emulsion closer to that ofthe heated water. All of these liquid products are then floweddownwardly through opening 11 and into compartment 12.

Compartment 12, similar to compartment 3, is basically characterized inthe opposite end of shell 1 by a vertical partition 13 which is parallelto partition 4. Also similar to compartment 3, second compartment 12 hasa heater 14 mounted therein. All the liquids flowing from compartment 3,along horizontal partition 10 are flowed downwardly over the tube ofheater 14, mounted as it is in compartment 12. Compartment 12 providesan additional, novel, function to this heating process.

The basic function of compartment 12 is to establish a collection of theliquid components of the well stream large enough to provide substantialresidence time and thermal agitation which will thoroughly mix theproduction, and any chemical added thereto, and complete the degassingof the production. Bringing the liquids downwardly over the tube of theheater 14 provides for degassing to occur in the upper regions of thebody of liquid within compartment 12. Evolving these gaseous componentsin the upper regions of this body of production tends to keep theliquids from being unduly agitated by the evolving gas.

The liquids of compartment 12 are heated by the tube of heater 14.Heater 14 is regulated as heater 5 in compartment 3 is regulated. Theheat output of heater 14 sets up thermal currents in the compartment 3liquids given the long residence time because of the capacity ofcompartment 3.

The thermal agitation in compartment 3 continues the mixing of theproduction and chemical. Additionally the thermal agitation will raisethe temperature of the pro duction to within the range which willcompletely prepare the production for optimum coalescence of its waterand oil. Also, substantially all of the gas to be evolved at the finaltreating temperature will be so evolved in the upper regions ofcompartment 12.

A temperature element 21 is indicated as positioned below the tube ofheater 14. Element 21 controls the gasfiring of heater .14, similar tothe control of heater 5 by element 6. It is contemplated that element 21will be located in the liquids of compartment 12 at a position where thecontrol exerted over heater 14 will result in bringing the liquids towithin the desired range of temperature as they leave the bottom ofcompartment 12 through opening 22.

The final heating afforded by heater 14 is accomplished efiiciently, andwith little coking and scaling on the heater tubes. The loweredviscosity provides a relatively high rate of heat transfer from thetubes of heater 14 to get the temperature at element 21 to within thedesired range of temperature with the minimum consumption of fuel. Thesuppression of the skin temperature of heater 14 to a minimum alsoresults in avoiding the coking and scaling on the surface of the heater14 which would take place, at higher skin temperatures.

Coking is basically a result of thermal decomposition of hydrocarbons.The lower the temperature to which the hydrocarbons are exposed, theless coking will occur. Therefore, the suppressed skin temperature ofheater 14 is a basic contribution to this result. Also, however, thethermal currents set up in compartment 12 promote oilwetting of thesurface of heater 14 by the agitation. Oilwetting of the surface ofheater =14 militates against scale.

Scale is basically a result of vaporizing mineral-carrying water in theproduction. The suppressed skin temperature, of course, reduces thescaling possibility. However, the oil-wetting of the surface of heater14 reduces the possibility of scale formation. Water has far lesstendency to vaporize on an oil-wetter surface and leave any mineralentrained therein. The thermal agitation in compartment 12 causes oil.to continually wipe the heater 14 surface and keep it wetted. Theresulting scale reduction follows.

The breaking of the union between the oil and water components of theproduction, which began in compartment 3, culminates in the lowerregions of compartment 12. The heat from the plurality of sourcesprovided in the compartments raises the temperature of the production,degasses the production and thoroughly mixes the production with anyemulsion-breaking chemical introduced therein. By the time theproduction has traveled down over heater 14 in compartment 12, a largepercentage of the water has been broken away from the oil. Thecollection of water at 23 represents, in part, that water which isprecipitated downwardly from compartment 12. This water is removedthrough conduit 24 in accordance with the control exerted by a float 25.The remaining emulsion passing through opening 22, from compartment 12,has been completely prepared for optimum coalescence within a structureprovided in a third compartment of vessel 1. I

All gaseous components evolved in the first compartment 3, Within theelongated passage of partition 10, and the upper regions of compartment12, are passed out shell 1 through a conventional mist extractorstructure 15 mounted in gas head 16. A heat exchanger 17 is mounted onthe top of gas head 16. All the gaseous components evolved are broughtinto heat exchanger 17 and into indirect contact with a stream ofcoolant. This stream of coolant is indicated as coming to heat exchanger17 through conduit 18 and leaving heat exchanger 17 through conduit 19.The coolant provided for heat exchangercondenser '17 may be from anycool stream of fluid available. The well stream of conduit 2 may wellhave a temperature adequate for this purpose. Of course, any cool streamof water available within the proper temperature range can be used.

It is comtemplated that all liquefiable components of the gaseous streampassing up through head 16 will fall back through head 16 and ontopartition 10. From partition 10, directly above compartment 12, thesecondensed liquids will join the liquids dropped into compartment 12through opening 11. The uncondensed portion of the gases up through head16 are removed from condensing heat exchanger 17 through conduit 20.Conduit 20 introduces these gaseous components back into shell 1 of thetreater. Should there be any liquid carry-over from exchanger 17,conduit 20 extends down into compartment 26 far enough to place theliquids well below the surface of the clean oil produced. Holes 20Aplace the gas from conduit 20 above the clean oil surface in compartment26.

Third compartment 26 is provided between first comhaving two sectionsdefined by horizontal imperforate' plates and expanded metal sections.The expanded met-a1 sections and imperfor-ate plates are arranged toprovide a serpentine path upward for the emulsion from compartment 12.The coalescing function of a hay section is well known. The globules ofoil agglomerated in this coalescing hay will migrate upward, and thedroplets of water agglomerated by the section will migrate downward tojoin the collected body of water 23. The result is to collect a body ofclean oil in the upper portion of compartment 26 above the hay sectionfrom which oil will be removed from vessel 1 by a skimmer 28 throughconduit 29.

The three compartments within shell 1 are illustrated in horizontalalignment. Obviously, it is feasible to provide separate vessels, ascompartments, which can be" connected by conduits through which to movethe fluids of the process. Arranged as they are, the three compartmentsof vessel II have the problem of forcing the clean oil from thecollection of oil in the upper portion of compartment .26. It isdifficult to provide a sufficient head for this purpose in a horizontalvessel. The present invention provides a substitute for this head force.

The uncondensed gases of conduit 20, from the top of exchanger-condenser17 are placed on the top of the clean oil surface in compartment 26through differential valve 30. Conduit 31 is provided to remove this gasfrom the surface of the clean oil in compartment 26 for disposal in anydesired manner. It is contemplated that the disposal location for thegases of conduit 31 has a pressure substantially less than the pressuredeveloped by the gases evolving up through the head 16 and intocondenser 17.

Therefore, a modulation of the position of valve 30' will:

develop a differential of pressure between the first two compartmentsand compartment 26 above the surface of the clean oil. This differentialof pressure will provide the force on the surface of the liquids incompartment 12 which will remove the liquids from compartment 12, intocompartment 26 and out conduit 29.

Diiferential valve 30 is modulated from'the level of supply from theconduit above horizontal partition 10,

fioat32 will develop a control pressure for differential valve 30 whichwill move valve 30 closed, increasing the diiferential pressure betweenthat pressure on the liquid surfaceof compartment 12 and that pressureon the oil surface of compartment 26. The result is to move liquids fromcompartment 12 to compartment 26 and remove oil through conduit 29. Asafety valve 33 is provided in conduit 34' between gas head 16 andconduit 31. This provision for the release of excess pressure withinshell 1 is desirable should the control system malfunction in themodulation of valve 30 or the hay section plug, or clog, with solidmatter.

FIG. 1 shows to advantage the unique arrangement of compartments withinshell 1 to provide a control of the temperature of liquids and gaseswithin compartment 26. Should water vapor be carriedfromexchanger-condenser 17 through conduit 20, it would be mostundesirable to condense this water vapor into the clean oil removedthrough conduit 29. Therefore, the arrangement illustrated in FIG. 1keeps the gas space above the clean oil in compartment 26 warm enough toprevent condensation of water vapor by reason of heat exchange with the7 liquids of compartment 13 which travel along partition directly abovecompartment 26 enroute to compartment 12.

FIG. 2 illustrates more completely the control float 32 has ondifferential valve 30 which it modulates. Additionally, a possibleposition for element 21 in compartment 12 is illustrated. Float 32 isshown as mechanically actuating a mechanical-fluid pressure transducer35 to produce a control fluid pressure in conduit 36 which can be placedon a diaphragm of valve 30 to modulate the position of the valve.

Referring now to FIG. 3, a modification of the FIG. 1 structure isillustrated, also embodying the invention. An elevated cross-section ofa shell 40 is shown to illustrate a treating vessel with a horizontallyextended longitudinal axis.

Oil well production is conducted into shell 40 through conduit 41 andspread, or dispersed, by the perforations of spreader 42. Spreader 42 ismounted in the bottom of compartment 43, from which position itdisperses production from conduit 41 upwardly through the liquids incompartment 43.

Heater 44 is mounted above spreader 42 to heat the liquids incompartment 43, along with the production from spreader 42. Baffles 45are mounted above heater 44 to mechanically manipulate the production asthe emulsion and gas is heated in its upward passage.

The temperature of the liquids in compartment 43 is controlled by asystem which fires heater 44 from the temperature sensed by element 46.The control system responsive to this temperature is similar to thatwhich includes element 6 in FIG. 1.

The complete process of manipulation and heating of the production incompartment 43 is similar to the process carried out in compartment 3 ofFIG. 1. Partition 47 defines the left limit of compartment 43 and theright limit is defined by the right end of vessel shell 40. It iscontemplated that compartment 43 will remain substantially full of waterwith which the dispersed production is heated as it travels upwardlythrough the water bath. Surplus water and production are withdrawnthrough opening 48 at the top of compartment 43. Thus, the productionreceives an initial treating by being heated by the water in compartment43, is mixed to an extent with any added chemical and has its viscositylowered and is degassed to an extent.

A tray 50 is mounted near the top of vessel 40, defining the top ofcompartment 43. Tray 50 is mounted at an angle to the horizontal axis ofthe vessel so that liquids from opening 48 will flow out of compartment43 and down over tray 50. Step-baffles 51 are placed at intervals alongtray 50, extending at right angles to the liquid flow. This arrangementprovides a cascading of the liquids which promotes additional degassingand mixing of the liquids. The degassed liquids from tray 50 are finallydropped downwardly over heater 52.

Heater 52 is mounted in a vessel compartment defined substantiallybetween horizontal partition 47 and horizontal partition 53. FIG. 4, isa cross-sectional elevation taken along lines 4--4 in FIG. 3 toillustrate that heater 52 is mounted generally at a right angle to thelongitudinal axis of vessel 40. This disclosure serves to illustrate theflexibility of the arrangement between heater 52 and its compartment 54which provides for adjusting the size of compartment 54, should this bedesired. If other considerations permit, this arrangement specificallyprovides for partitions 47 and 53 to be placed close together, incontrast the FIG. 1 arrangement, to form a compartment 54 which isrelatively small. At least one result of this arrangement is thepossibility of establishing an over-all length of vessel 40 which ismaterially less than that of vessel 1. In any event, compartment 54functions generally in the same manner as compartment 12 of FIG. 1.

The production from compartment 43 flows downwardly over heater 52 incompartment 54. Additional gas is released in the upper regions of thecompartment 54. The firing of heater 52 is controlled from element 55 inbringing the production up to treating temperature as it passes outopening 56 to the coalescing section. The thermal agitation by heater52, the mixing of the production and any added chemical, the finalevolvement of gas in the upper regions of compartment 54, the avoidanceof coking and scaling, the lowered fuel consumption by heater 52 and thefinal preparation of the production for optimum coalescence all takeplace in compartment 54 as they do in compartment 12 of FIG. 1.

All gaseous components evolved are passed out of shell 40 through mistextractor 57 mounted in head 58. Heat exchanger 59 functions to liquefya portion of the gas after the fashion of exchanger 17 in FIG. 1. Theliquid condensed falls into compartment 54 to maintain the gravity ofthe final clean oil product of the process.

The third compartment 69 is provided between partitions 53 and 61 forthe coalescing section. The coalescing section is formed of hay, orexcelsior, at 62, as in compartment 26 of FIG. 1. Battles, as indicated,may form a serpentine path upward for the oil, through section 62. Thebody of clean oil above the section 62 discharges over the upper edge ofpartition 61 as a weir. In contrast to the FIG. 1 arrangement,compartment 60 is arranged between compartment 54 and the left end ofvessel 40, rather than between the two heating compartments in which theheating of the production is staged. This arrangement retains benefitsof the up-flow, down-flow stage heating while providing for heater 52 tobe inserted in the compartment 54 from the side of vessel shell 40 inmaking a more compact arrangement.

The clean oil flowing from section 60, over the upper weir edge ofpartition 61, collects between partition 61 and the left end of thevessel shell 40, in a body 63. Clean oil is drawn from this collectionthrough conduit 64, valved under the control of float 65.

The gas evolved in the compartments of 43 and 54, are passed out of head58 and exchanger 59 and into conduit 66. Conduit 66 passes through valve67, and conduit 66 introduces the evolved gas into the space above theclean oil in the compartment 60. All gas to the left of partition 53 isremoved through conduit 68. Valve 67 is positioned by a control signaldeveloped by the response of float 68 to the level of the liquids incompartment 54.

FIG. 4 shows float 69 to further advantage, responding to the liquidlevel in compartment 54 to develop a fluid pressure with control unit 70for the diaphragm of valve 67. Controlled in this manner, valve 67restricts conduit 66 enough to maintain suificient differential betweenthe gas pressures on the liquid surfaces of compartments 54 and 60 toovercome the variable restrictions to liquid flow to the coalescingsection 60. The liquid level in compartment 54 is an excellent end-pointindex of all variables of the process which affect the flow of liquidsthrough the vessel 40. These variables may be in the variation in theproduction of flow through conduit 41, or in resistance to flow throughcoalescing section 60. The resistance to flow through coalescing section60 may be due either to the flow friction due to temperature variationor the mechanical impediment of solid particles in the section. In anyevent, all these variables influence the liquid level in compartment 54,and, therefore, are automatically applied to positioning of valve 67 inmaintaining a dynamic fluid pressure force to move the liquids out ofthe vessel 40. i

From the foregoing it will be seen that this invention is one welladapted to attain all of the ends and objects hereinabove set forth,together with other advantages which are obvious and which are inherentto the apparatus.

It will be understood that certain features and subcombinations are ofutility and may be employed without 9 reference to other features andsubcombinations. This is contemplated by and it within the scope of theclaims.

As many possible embodiments may be made of the invention withoutdeparting from the scope thereof, it is to be understood that all matterherein set forth or shown in the accompanying drawings is to beinterpreted as illustrative and not in a limiting sense.

The invention having been described, what is claimed 1. The method oftreating oil well production including, maintaining a body of waterwithin a first predetermined range of temperature with a first source ofheat, passing oil well production up through the body of water to lowerthe viscosity of the production to where foam of the production will beeffectively reduced, passing water of the heat-ed body and productionalong an elongated common path, after first heating, maintaining a bodyof the production within a second predetermined range of temperaturewith a second source of heat, passing the water and production from theelongated common path down through the body of the production withresidence time sufiicient to thoroughly mix the production by thermalcurrents created by the second source of heat and to further degas theproduction and to prepare the production for coalescence, passing theproduction through a zone of coalescence to coalesce the oil and migrateit upward and coalesce the water and migrate it downward, andmaintaining vapors evolved from the body of oil above the coalescencezone in heat transfer relationship with the hot water and production inthe common path to prevent condensation of water vapor directly onto thesurface of the oil.

2. The method of claim 1 including, developing a pressure differentialacross the zone of coalescence to force the oil out of the coalescencezone.

3. The method of claim 2 including, developing the pressure differentialacross the zone of coalescence with the level of the body of theproduction within the second predetermined range of temperature.

4. The method of claim 3 including, adding an ernulsion-breakingchemical to the production prior to passing the production up throughthe body of Water heated to the first predetermined range oftemperature.

5. The method of claim 3 including, removing the hydrocarbon vapors fromthe degassed production, cooling the hydrocarbon vapors to condense theportion of them which can be stored under substantially ambienttemperatures and pressures, and returning the liquids condensed to thebody of production within the second predetermined range of temperature.

6. The method of claim 5 in which the cooling of the hydrocarbon vaporsis obtained by heat transfer with the oil well production going to thebody of water heated to a first predetermined range of temperature.

7. The method of treating oil well production including, heating a bodyof water to within a first predetermined range of temperature with afirst source of heat, dispersing a foamy oil well production upwardlythrough the heated body of water to lower the viscosity of theproduction to where the foam will be effectively reduced, passing theproduction downwardly over a second source of heat in a body ofproduction heated to a second predetermined range of temperature and ofa size to give a residence time which will enable the thermal currentsdeveloped by the second source of heat to roll and mix and degas theproduction to a substantial degree, controlling the release of gas fromthe first and second heating to develop a force on the surface of theproduction heated to the second predetermined range of temperature tomaintain the level of the surface at a predetermined height, passing theproduction from the body heated to the second predetermined range oftemperature upwardly through a coalescence zone and collecting the oilabove the zone and withdrawing the oil from the process, and maintainingthe collected oil and 10 vapor above the collected oil in heat transferrelationship with the production and water from the heated body of waterto prevent condensation of water from the vapor v into the oil collectedand withdrawn.

liquids to the body of production heated to the second predeterminedrange of temperature.

10. The method of treating oil well production including, maintaining abody of water within a first predetermined range of temperature with afirst source of heat,

controlling the firing rate of the first source of heat to maintain theskin temperature of the first heat source below that at which cokingwill occur on the surface of the first heat source, passing oil wellproduction up through the body of water to lower the viscosity of theproduction to where foam of the production will be effectively reduced,maintaining a body of the production within a second predetermined rangeof temperature with a second source of heat, controlling the fin'ng rateof the second source of heat to maintain the skin temperature of thesecond heat source below that at which coking will occur on the surfaceof the second heat source, passing the water and production from thefirst body of water down through the body of production with residencetime sufiicient to thoroughly mix the production by thermal currentscreated by the second source of heat and to further degas the productionand to prepare the production for coalescence, flowing the brokenemulsion through a zone of coalescence to coalesce the oil and migrateit upward and coalesce the water and migrate it downward, andwithdrawing the gas and water and oil separately. I

11. The method of claim 10 including, developing a pressure differentialacross the zone of coalescence to force the oil out of the coalescencezone.

12. The method of claim 11 including, developing the pressuredilferential across the zone of coalescence with the level of liquidswithin the second predetermined range of temperature.

13. The method of claim 12 including, adding an emulsion-breakingchemical to the oil well emulsion prior to flowing upwardly all of theproduction be treated through the body of water within the firstpredetermined range of temperature.

14. The method of claim 13 including, cooling the withdrawn gas tocondense storageable liquid hydrocarbons and returning the liquids tothe emulsion passed downwardly through the body of production within thesecond predetermined range of temperature.

15. The method of treating oil well production including maintaining abody of Water within a first predetermined range of temperature with afirst source of heat, controlling the firing rate of the first source ofheat to maintain the skin temperature of the first heat source belowthat at which coking will occur on the surface of the first heat source,passing oil well production up through the body of water to lower theviscosity of the production to where foam of the production will beeffectively reduced, maintaining a body of the production within asecond predetermined range of temperature with a second source of heat,controlling the firing rate of the second source of heat to maintain theskin temperature of the second heat source below that at which cokingwill occur on the surface of the second heat pare the production forcoalescence, flowing the broken emulsion upwardly through a zone ofcoalescence between the body of water within the first predeterminedrange of temperature and the body of production within the secondpredetermined range of temperature to heat exchange with the brokenemulsion while oil is coalesced and migrated upward and water iscoalesced and migrated downward, and withdrawing the gas and water andoil separately.

16. The method of claim 15 including, developing a pressure differentialacross the zone of coalescence to force the oil out of the coalescencezone.

17. The method of claim 16 including, developing the pressuredifferential across the zone of coalescence with the level of liquidswithin the second predetermined range of temperature.

18. The method of claim 17 including, adding an emulsion-breakingchemical to the oil well emulsion prior to flowing upwardly all of theproduction to be treated through the body of water within the firstpredetermined range of temperature.

19. The method of claim 18 including, cooling the withdrawn gas tocondense storageable liquid hydrocarbons and returning the liquid to theemulsion passed downwardly through the body of production within thesecond predetermined range of temperature.

20. Apparatus for the treatment of oil well production including, afirst chamber into which the production is received, a body of water inthe first chamber, a first source of heat for the body of water, meansfor regulating the first source of heat to raise the temperature of theproduction passed up through the body of water to lower the viscosity ofthe production to where foam of the production will be effectivelyreduced, a second chamber into which water from the body of water in thefirst chamber and the production is received, a second source of heatfor the production in the second chamber passed downwardly over thesecond source of heat, means for regulating the second source of heat toproduce thermal currents in the production to further degas theproduction and to prepare the production for coalesence, a third chamberto receive the production and coalesce the oil and migrate it upward andcoalesce the water and migrate it downward, and a conduit between thefirst and second chambers in heat exchange relationship with the thirdchamber so the heat of the water and production from the first chamberwill prevent condensation of any water vapor above the coalesced oilinto the oil.

21. The apparatus of claim 20 including, means responsive to the levelof production in the second chamber controlling the release of gas fromthe chambers to develop a diiferential pressure across the third chamberto force the oil from the third chamber.

22. The apparatus of claim 20 including, means for adding apredetermined amount of emulsion-breaking chemical to the productionprior to the production being received in the first chamber.

23. The apparatus of claim 21 including, a condenser receiving thehydrocarbon vapors from the degassed production to condense that part ofthem which can be stored under substantially ambient temperatures andpressures, and means for returning the condensed liquids to the secondchamber.

24. The apparatus of claim 23 including, means for supplying the oilwell production to the first chamber to the condenser as a heat exchangemedium with which to condense the hydrocarbon vapors.

25. Apparatus for treating oil well production including, a first sourceof heat, a body of water heated to within a first predetermined range oftemperature by the first source of heat, means for dispersing a foamyoil well production upwardly through the heated body of water to lowerthe viscosity of the production until the foam is effectively reduced, asecond source of heat, means for passing the defoamed productiondownwardly over the second source of heat and maintaining the productionheated in a body of a size to give a residence time which will enablethe thermal currents developed to roll and mix and further degas theproduction to a substantial degree, means to control the release of gasfrom the first and second heating to develop a force on the surface ofthe production passed downwardly over the second source of heat whichwill maintain the level at a predetermined height, means defining acoalescence zone, means passing the production from the second source ofheat upwardly through the coalescence zone to collect oil at the top ofthe zone and withdraw the oil from the process, and means arranging thedefoamed production from the first heating in heat exchange relationshipwith the top of the coalescence zone to prevent condensation of waterfrom the vapor at the top of the zone into the coalesced oil.

26. The apparatus of claim 25 including, means for adding apredetermined amount of emulsion-breaking chemical to the productionprior to dispersing the production through the body of heated water.

27. The apparatus of claim 25 including, a condenser arranged to coolthe gas released from the production by the heating and condensestorageable liquids therefrom, and means for returning the liquid to thedefoamed production which was passed downwardly over the second sourceof heat.

28. Apparatus for the treatment of oil well production including, afirst chamber into which the production is received, a body of water inthe first chamber, a first source of heat for the body of water, meansregulating the first source of heat to raise the temperature of theproduction passed up through the body of water to lower the viscosity ofthe production to where foam of the production will be effectivelyreduced while not elevating the skin temperature of the first heatsource so high as to produce coking on the surface of the first heatsource, a second chamber into which water from the body of water in thefirst chamber and the production is received, a second source of heatfor the production in the second chamber passed downwardly over thesecond source of heat, means regulating the second source of heat toproduce thermal currents in the production to further degas theproduction and to prepare the production for coalescence while notelevating the skin temperature of the second heat source so high as toproduce coking on the surface of the second heat source, a third chamberreceiving the production from the second chamber to coalesce the oil andmigrate it upward and coalesce the water and migrate it downward, andmeans for withdrawing the gas and water and oil separately.

29. The apparatus of claim 28 including, means with which a pressuredifferential is developed between the second and third chambers to forcethe oil out of the third chamber.

30. The apparatus of claim 29 in which, the means developing thepressure differential is directly responsive to the level of liquids ofthe second chamber.

31. The apparatus of claim 28 including, a condenser receiving the gasevolved from the first and second chambers to condense storageableliquid hydrocarbons therefrom and return those liquids to the secondchamber.

32. The apparatus of claim 28 including, a means for adding apredetermined amount of emulsion-breaking chemical to the oil wellemulsion prior to flowing upwardly all the products to be treatedthrough the first chamber.

33. Apparatus for the treatment of oil well production including, afirst chamber into which the production is received, a body of water inthe first chamber, a first source of heat for the body of water, meansregulating the first source of heat to raise the temperature of theproduction passed up through the body of water to lower the viscosity ofthe production to where foam of the production will be effectivelyreduced while not elevating the skin temperature of the first heatsource so high as to produce coking on the surface of the first heatsource, a second chamber into which water from the body of water in thefirst chamber and the production is received, a second source of heatfor the production in the second chamber passed downwardly over thesecond source of heat, means regulating the second source of heat toproduce thermal currents in the production to further degas theproduction and to prepare the production fior coalescence while notelevating the skin temperature of the second heat source so high as toproduce coking on the surface of the second heat source, a third chamberin the unified vessel located between the first and second chambers andin heat exchange relation to them while oil is coalesced and migratedupward and water is coalesced and migrated downward, and conduitsconnected to the second and third chambers through which gas and oil andwater are separately removed.

34. The apparatus of claim 33 including, means for developing a pressuredifferential between the second chamber and the third chamber to forceoil from the third chamber in its conduit.

35. The apparatus of claim 34 in which the means developing the pressuredifierential responds to the level of the liquids in the second heatingzone.

36. The apparatus of claim 34 including, means for adding apredetermined quantity of emulsion-breaking chemical to the oil wellemulsion prior to flowing all of the products to be treated through thefirst chamber.

37. The apparatus of claim 35 including, a heat exchanger for coolingthe gas of the process sufiiciently to condense storageable liquidhydrocarbons from the gas and returning the liquids to the emulsionpassed to the second chamber.

38. A horizontal treater for oil well emulsions including, a firstcompartment in the treater shell, a first firetube in the firstcompartment controlled to raise the temperature of emulsion flowingupwardly over the firetube to reduce the viscosity of the emulsion andevolve hydrocarbon and water vapors, a second compartment in the treatershell, a second firetube in the second compartment controlled to furtherraise the temperature of the emulsion flowed downwardly over thefiretube from the first compartment until the emulsion film is broken aswater is removed downwardly at a rate which militates againstsubstantially heating the water further, a third compartment in thetreater shell into which the oil and broken emulsion of the secondcompartment is flowed for coalescence of the oil in its top and water inits bottom, a condenser receiving the evolved vapors from the first andsecond compartments to condense the storageable liquid hydrocarbons fromthe evolved vapors, and return the liquid to the second chamber, aconduit for removing any uncondensed vapor and liquid carryover from thecondenser and placing the vapor in the third compartment above the oilsurface and the liquid in the third compartment below the oil surface,and conduits connected to the second and third compartments forwithdrawing the gas and water and oil separately.

39. The treater of claim 38 including, a coalescing structure in thethird compartment, a valve in the conduit between the condenser and thethird compartment, and a level responsive means in the secondcompartment detecting the liquid level controlling the valve to developa pressure differential between the second and third compartments whichwill force the emulsion from the second compartment and the oil from thethird compartment.

References Cited in the file of this patent UNITED STATES PATENTS2,598,988 Glasgow June 3, 1952 2,601,903 Erwin July 1, 1952 2,601,904Erwin July 1, 1952 2,664,170 Walker et al Dec. 29, 1953 2,713,919 Walkeret a1 July 26, 1955 2,751,998 Glasgow June 26, 1956

